Catalyst from flame-spray pyrolysis and catalyst for autothermal propane dehydrogenation

ABSTRACT

The invention relates to a method of production of catalyst particles, comprising platinum and tin and also at least one further element, selected from lanthanum and cesium, on zirconium dioxide as support, comprising the steps: preparation of one or more solutions containing precursor compounds of Pt, Sn and at least one further element of La or Cs and also ZrO 2 , converting the solution(s) to an aerosol, bringing the aerosol into a directly or indirectly heated pyrolysis zone, carrying out pyrolysis, and separation of the particles formed from the pyrolysis gas. 
     Suitable precursor compounds comprise zirconium(IV) acetylacetonate, lanthanum(II) acetylacetonate and cesium acetate, hexamethyldisiloxane, tin 2-ethylhexanoate, platinum acetylacetonate, zirconium(IV) propylate in n-propanol and lanthanum(II) acetylacetonate. 
     The invention also relates to the catalyst particles obtainable using the method according to the invention, and to the use thereof as dehydrogenation catalysts.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a divisional application of U.S. Non-ProvisionalApplication No. 13/356,787, filed Jan. 24, 2012, which claims thebenefit (under 35 USC 119(e)) of U.S. Provisional Application61/435,797, filed Jan. 25, 2011, the contents of each of which areincorporated herein by reference in their entireties.

BACKGROUND OF THE INVENTION

The invention relates to catalyst particles, a method of productionthereof and the use of the catalyst particles as dehydrogenationcatalyst.

Production of dehydrogenation catalysts by impregnation processes orspray drying is known. In these methods the catalytically active metalsare applied on an oxide support or a silicate support by impregnationprocesses or the catalyst is produced by spray drying of coprecipitatedoxide precursors.

DE-A 196 54 391 describes the production of a dehydrogenation catalystby impregnation of essentially monoclinic ZrO₂ with a solution ofPt(NO₃)₂ and Sn(OAc)₂ or by impregnation of ZrO₂ with a first solutionof Pt(NO₃)₂ and then a second solution of La(NO₃)₃. The impregnatedsupports are dried and then calcined. The catalysts thus obtained areused as dehydrogenation catalysts for the dehydrogenation of propane topropene.

A known method of production of metal catalysts by flame-spray pyrolysisis described in Pisduangnawakij et al., Applied Catalysis A: General 3701-6, 2009. In this, a solution containing precursor compounds ofplatinum and tin and of aluminum oxide as support in xylene is convertedto an aerosol, this is treated in an inert carrier gas in a pyrolysisreactor at a temperature above the decomposition temperature of theprecursor compounds and then the finely-divided metal that has formed isseparated from the carrier gas.

The known synthesis of precious metal powder catalysts by wet-chemicalpreparation is time-consuming and costly.

The methods for the production of dehydrogenation catalysts aretherefore still in need of improvement in terms of the time and coststhey involve.

A SUMMARY OF THE INVENTION

The problem to be solved by the present invention is to provide aninexpensive and time-saving method of production of dehydrogenationcatalysts, wherein the dehydrogenation catalysts obtained should becomparable in activity and selectivity to the catalysts of the priorart, produced by impregnation processes or spray drying.

This problem is solved by a method of production of catalyst particles,comprising platinum and tin and also at least one further element,selected from lanthanum and cesium, on a support comprising zirconiumdioxide, comprising the steps

(i) preparation of one or more solutions containing precursor compoundsof platinum, tin and the at least one further element, selected fromlanthanum and cesium, and also of zirconium dioxide,(ii) converting the solution(s) to an aerosol,(iii) bringing the aerosol into a directly or indirectly heatedpyrolysis zone,(iv) carrying out pyrolysis, and(v) separation of the particles formed from the pyrolysis gas.

A BRIEF DESCRIPTION OF THE FIGURE

FIG. 1 illustrates activities and selectivities for theflame-synthesized catalysts (▴ example 13, ▪ example 17) and for thereference catalyst (−) in the autothermal dehydrogenation of propane topropene.

A DETAILED DESCRIPTION OF THE INVENTION

The metal compounds and oxide-forming precursor compounds are fed asaerosol to the pyrolysis zone. It is preferable if the aerosol fed tothe pyrolysis zone is obtained by nebulization of just one solution,which contains all the metal compounds and oxide-forming precursorcompounds. In this way it is always ensured that the composition of theparticles produced is homogeneous and constant. During preparation ofthe solution that is to be converted to an aerosol, the individualcomponents are thus preferably selected so that the oxide-formingprecursors and the precious metal compounds used contained in thesolution are dissolved uniformly alongside one another untilnebulization of the solution. Alternatively it is also possible to useseveral different solutions, which, on the one hand, contain theoxide-forming precursors and, on the other hand, contain the active orpromoter metal compounds. The solution or solutions can contain bothpolar and apolar solvents or solvent mixtures.

In the pyrolysis zone, decomposition of the precious metal compound toform the precious metal and decomposition and/or oxidation of the oxideprecursors, with formation of the oxide, take place. It may also happenthat some of the precious metal evaporates and then redeposits in coolerzones on support particles already formed. Pyrolysis generally resultsin spherical particles with varying specific surface.

The temperature in the pyrolysis zone is above the decompositiontemperature of the precious metal compounds at sufficient temperaturefor oxide formation, usually between 500 and 2000° C. Pyrolysis ispreferably carried out at a temperature from 900 to 1500° C.

The pyrolysis reactor can be heated indirectly from outside, for exampleby means of an electric furnace. Owing to the temperature gradient fromoutside to inside that is required in indirect heating, the furnace mustbe much hotter than corresponds to the temperature required forpyrolysis. Indirect heating requires a thermally stable furnace materialand an expensive reactor construction, but the total amount of gasrequired is less than in the case of a flame reactor.

In a preferred embodiment the pyrolysis zone is heated by a flame(flame-spray pyrolysis). The pyrolysis zone then comprises an ignitiondevice. For direct heating, usual combustible gases are used, althoughpreferably hydrogen, methane or ethylene is used. The temperature in thepyrolysis zone can be adjusted as required by means of the ratio of theamount of combustible gas to the total amount of gas. To keep the totalamount of gas low but nevertheless achieve a temperature as high aspossible, the pyrolysis zone can also be supplied with pure oxygeninstead of air as the O₂ source for combustion of the combustible gases.The total amount of gas also comprises the carrier gas for the aerosoland the evaporated solvent of the aerosol. The aerosol or aerosolssupplied to the pyrolysis zone are preferably fed directly into theflame. Although air is generally preferred as carrier gas for theaerosol, it is also possible to use nitrogen, CO₂, O₂ or a combustiblegas, for example hydrogen, methane, ethylene, propane or butane.

In another embodiment of the method according to the invention, thepyrolysis zone is heated by an electric plasma or an inductive plasma.In this embodiment, the catalytically active precious metal particlesare deposited on the surface of the support particles and are fixedfirmly thereon.

A flame-spray pyrolysis device generally comprises a storage containerfor the liquid to be nebulized, feed pipes for carrier gas, combustiblegas and oxygen-containing gas, a central aerosol nozzle, and an annularburner arranged around this, a device for gas-solid separationcomprising a filter element and a discharging device for the solid andan outlet for the exhaust gas. The particles are cooled by means of aquench gas, e.g. nitrogen or air.

The pyrolysis zone preferably comprises a so-called pre-drier, whichsubjects the aerosol to preliminary drying before its entry into thepyrolysis reactor, this preliminary drying taking place, for example, ina flow tube with a heating assembly disposed around it. Wherepreliminary drying is not carried out, the risk exists of obtaining aproduct with a relatively broad particle size spectrum, and moreparticularly an excessive fine fraction. The temperature of thepre-drier is dependent on the nature of the dissolved precursors and onthe concentration thereof. The temperature in the pre-drier is typicallyabove the boiling point of the solvent, up to 250° C.; in the case ofwater as a solvent, the temperature in the pre-drier is preferablybetween 120 and 250° C., more particularly between 150 and 200° C. Thepre-dried aerosol, supplied to the pyrolysis reactor via a line, thenenters the reactor via an exit nozzle.

To produce a balanced temperature profile, the combustion space, whichis preferably tube-shaped, is heat-insulated.

As the pyrolysis result, a pyrolysis gas is obtained, which containsspherical particles with varying specific surface. The size distributionof the pigment particles obtained results essentially directly from thedroplet spectrum of the aerosol fed into the pyrolysis zone and theconcentration of the solution or solutions used.

Preferably, prior to separation of the particles formed from thepyrolysis gas, the pyrolysis gas is cooled so that sintering together ofthe particles is excluded. For this reason the pyrolysis zone preferablycomprises a cooling zone, which adjoins the combustion space of thepyrolysis reactor. Cooling of the pyrolysis gas and of the catalystparticles contained therein to a temperature of about 100-500° C. isgenerally required, depending on the filter element used. Cooling toapprox. 100-150° C. preferably takes place. After leaving the pyrolysiszone, the pyrolysis gas, containing catalyst particles, and partiallycooled, enters a device for separating the particles from the pyrolysisgas, which comprises a filter element. For cooling, a quench gas, forexample nitrogen, air or water-moistened air, is fed in.

Suitable zirconium dioxide—forming precursor compounds are alcoholates,such as zirconium(IV) ethanolate, zirconium(IV) n-propanolate,zirconium(IV) isopropanolate, zirconium(IV) n-butanolate andzirconium(IV) tert-butanolate. In a preferred embodiment of the methodaccording to the invention, zirconium(IV) propanolate, preferably assolution in n-propanol, is used as ZrO₂ precursor compound.

Other suitable zirconium dioxide—forming precursor compounds arecarboxylates, such as zirconium acetate, zirconium propionate, zirconiumoxalate, zirconium octoate, zirconium 2-ethyl-hexanoate, zirconiumacetate, zirconium propionate, zirconium oxalate, zirconium octanoate,zirconium 2-ethylhexanoate, zirconium neodecanoate zirconium stearateand zirconium propionate. In another preferred embodiment of the methodaccording to the invention, zirconium(IV) acetylacetonate is used asprecursor compound.

In one embodiment, the precursor compounds additionally comprise asilicon dioxide precursor compound. Possible precursors for silicondioxide are organosilanes and reaction products of SiCl₄ with loweralcohols or lower carboxylic acids. It is also possible to usecondensates of the aforementioned organosilanes and/or -silanols withSi—O—Si units. Siloxanes are preferably used. It is also possible to useSiO₂. In a preferred embodiment of the method according to theinvention, the precursor compounds comprise hexamethyldisiloxane assilica-forming precursor compound.

Besides zirconium dioxide and optionally silicon dioxide as supports,the catalyst particles according to the invention further compriseplatinum and tin and also at least one further element, selected fromlanthanum and cesium.

In one preferred embodiment of the invention, the Pt loading is 0.05 to1 wt. % and the Sn loading is 0.05 to 2 wt. %.

Preferred precursor compounds for lanthanum and cesium, respectively,are carboxylates and nitrates, corresponding for example to thecarboxylates identified above in connection with zirconium. In onepreferred embodiment of the method according to the invention, theprecursor compounds comprise lanthanum(III) acetylacetonate and/orcesium acetate.

In a further, preferred embodiment of the method according to theinvention, the precursor compounds comprise lanthanum(III)2-ethylhexanoate.

Preferred precursor compounds for tin are carboxylates and nitrates,corresponding for example to the carboxylates identified above inconnection with zirconium. In a further, preferred embodiment of themethod according to the invention, the precursor compounds comprise tin2-ethylhexanoate.

Preferred precursor compounds for platinum are carboxylates andnitrates, corresponding for example to the carboxylates identified abovein connection with zirconium, and ammonium platinates. In a preferredembodiment of the method according to the invention, the precursorcompounds comprise platinum acetylacetonate.

Both polar and apolar solvents or solvent mixtures can be used forproduction of the solution or solutions required for aerosol formation.

Preferred polar solvents are water, methanol, ethanol, n-propanol,iso-propanol, n-butanol, tert-butanol, n-propanone, n-butanone, diethylether, tert-butyl-methyl ether, tetrahydrofuran, C₁—C₈ carboxylic acids,ethyl acetate and mixtures thereof.

In a preferred embodiment of the method according to the invention, oneor more of the precursor compounds, preferably all the precursorcompounds are dissolved in a mixture of acetic acid, ethanol and water.Preferably this mixture contains 30 to 75 wt. % acetic acid, 30 to 75wt. % ethanol and 0 to 20 wt. % water. In particular, zirconium(IV)acetylacetonate, hexamethyldisiloxane tin 2-ethylhexanoate, platinumacetylacetonate, lanthanum(II) acetylacetonate and cesium acetate aredissolved in a mixture of acetic acid, ethanol and water.

Preferred apolar solvents are toluene, xylene, n-heptane, n-pentane,octane, isooctane, cyclohexane, methyl, ethyl or butyl acetate ormixtures thereof. Hydrocarbons or mixtures of hydrocarbons with 5 to 15carbon atoms are also suitable. Xylene is especially preferable.

In particular, Zr(IV) propylate, hexamethyldisiloxane tin2-ethylhexanoate, platinum acetylacetonate and lanthanum(III)acetylacetonate are dissolved in xylene.

The present invention also relates to the supports and catalystparticles obtainable by the method according to the invention. Thesepreferably have a specific surface of 20 to 70 m²/g.

In a preferred embodiment the catalyst particles have the followingpercentage composition: 30 to 99.5 wt. % ZrO₂ and, 0.5 to 25 wt. % SiO₂as support, 0.1 to 1 wt. % Pt, 0.1 to 10 wt. % Sn, La and/or Cs,relative to the mass of the support, wherein at least Sn and La or Csare contained.

The present invention also relates to the use of the catalyst particlesas hydrogenation catalysts or dehydrogenation catalysts. Alkanes, suchas butane and propane, but also ethylbenzene, are preferablydehydrogenated.

The use of the catalysts according to the invention for thedehydrogenation of propane to propene is especially preferred.

The invention is explained in more detail with the following examples.

Examples

Chemicals used

Zirconium acetylacetonate Zr(acac)₂ (98%)

Zirconium(IV) propoxide Zr(OPr)₄ (70% in 1-propanol)

Hexamethyldisiloxane (HMDSO) (98%)

Tin(II) 2-ethylhexanoate (approx. 95%)

Platinum(II) acetylacetate (98%)

Lanthanum(III) 2-ethylhexanoate (10% w/v)

Lanthanum(III) acetylacetonate (99.99%)

Cesium acetate (99.99%)

Mixture of acetic acid (100%), ethanol (96%) and water (deionized)

Xylene (BASF, mixture of isomers)

Preparation of the Solutions of the Precursor Compounds

The solvent is HoAc: EtOH: H₂O in the proportions by weight 4.6 to 4.6to 1. The acetic acid-ethanol mixture is freshly prepared. The precursorcompounds for Sn, Cs, La, Si, Pt and Zr are dissolved therein.

The composition of the polar solutions of the precursor compounds forthe examples 1, 2, 3, 9 and 10 is shown in Table 1.

TABLE 1 Compositions of the solutions of the precursor compounds forpolar mixtures (EtOH:HoAc:H₂O) [g] Substance Purity [wt. %] 99.52Zirconium(IV) acetylacetonate 98 1.77 Hexamethyldisiloxane 99 0.93 Tin2-ethylhexanoate 95 0.27 Platinum acetylacetonate 98 2.45 Lanthanum(III)acetylacetonate 99.9 0.38 Cesium acetate 99.99

For preparing the solution of the precursor compound for example 4, thefollowing substances were dissolved in xylene. The composition is shownin Table 2.

TABLE 2 Compositions of the solutions of the precursor compounds forapolar mixtures (xylene) [g] Substance Purity [wt. %] 374.40 Zr(IV)propylate in n-propanol 70 10.11 Hexamethyldisiloxane 99 5.32 Tin2-ethylhexanoate 95 1.52 Platinum acetylacetonate 98 103.47Lanthanum(III) 2-ethylhexanoate 10

In the case of the preparation of the solutions of the precursorcompounds for examples 5, 6 and 8, an additional 2.14 g of cesiumacetate are used as well.

Examples 1 to 10

Production of the catalyst particles by flame-spray pyrolysis

The solution containing the precursor compounds was supplied by means ofa piston pump via a two-component nozzle and atomized with acorresponding amount of air. To reach the corresponding temperatures,sometimes a support flame from an ethylene-air mixture was used, whichwas supplied via an annular burner located around the nozzle. Thepressure drop was kept constant at 1.1 bar.

The flame synthesis conditions are summarized in Table 3.

TABLE 3 Test parameters relating to the production of flame-spraypyrolysis catalysts c_(Zr) Flow rate Total Dispersion [mol/kg ofprecursor gas flow gas flow Ethylene Example Solvent solution] compound[l/h] [l/h] [l/h] GLMR¹ 1 HoAc, EtOH, 0.5 500 3500 1200 40  3 H₂O 2HoAc, EtOH, 0.5 510 3500 1200 20-40 3 H₂O 3 HoAc, EtOH, 0.2 515 35001200 10-50 3 H₂O  4* Xylene 1 280 3500 1200 0 5 5 Xylene 1 290 3500 12000 5 6 Xylene 1 310 3500 1200 0 4  7** Xylene 1 310 3500 1200 0 4 8Xylene 1 255 3500 1200 20-40 5 9 HoAc, H₂O 0.2 520 3500 1200 130-120 310  HoAc, H₂O 0.25 385 4140 1740 190-230 5 Solution without cesiumprecursor compound **Only Si and Zr precursors present ¹GLMR = Gas toLiquid Mass Ratio.

A baghouse filter was used for separating the particles. These filterscould be cleaned by applying 5 bar pressure surges of nitrogen to thefilter bags.

Particle characterization was carried out by means of X-raydiffractometry (XRD) and BET measurement, and an element analysis wascarried out as well. The crystallite size of the catalyst particlesformed using the solution of the precursor compounds 3 and 4 is set outin Table 4.

TABLE 4 X-ray powder diffractometry for the characterization of the ZrO₂Crystal- Crystal- Average Precursor Tetragonal Monoclinic lite size,lite size crystal- compound ZrO₂ ZrO₂ tetragonal monoclinic lite sizeused [%] [%] [nm] [nm] [nm] 3 82 18 19 13 18 4 90 10 28 9 26

The syntheses of the catalysts from the above solutions comprisingprecursor compounds with the settings specified above produced particleshaving a specific surface area of 36-70 m²/g (see Table 5).

In a further experiment, the BET surface area was investigated as afunction of the temperature of the combustion chamber. This involved acomparison of the solutions comprising the precursor compounds, in termsof their solvent (acetic acid versus xylene). In the case of the aceticacid mixtures, there was no clear trend apparent.

The xylene mixtures exhibited an increasing BET surface area withincreasing temperature, and this may be attributed to a shorterresidence time, thereby restricting particle growth.

Examples 11 to 17 Catalytic Measurements

Propane dehydrogenation was carried out at approx. 600° C. (Flows at 20ml cat. volume, mass see Table 5): 21 Nl/h total gas (20 Nl/h propane, 1Nl/h nitrogen as internal standard), 5 g/h water. Regeneration iscarried out at 400° C. as follows: 2 hours 21 Nl/h N₂+4 Nl/h air; 2hours 25 Nl/h air; 1 hour 25 Nl/h hydrogen.

The support of the reference catalyst from hydrothermal synthesis (ZrO₂)with subsequent spray drying is composed of 95% ZrO₂ and 5% SiO₂. Theactive/promoter metals are 0.5% Pt, 1% Sn, 3% La, 0.5% Cs and 0.2% K,and were applied to the support wet-chemically by impregnation inaccordance with the instructions of EP 1 074 301, example 4.

The conversion, the long-term stability and the selectivity of propeneformation were investigated in the catalytic tests. The results aresummarized in Table 5. The activities and selectivities relate to anoptimum operating state.

TABLE 5 Catalyst results for the flame-synthesized catalyst particles inautothermal propane dehydrogenation Mass of Catalyst used BET ActivitySelectivity Example catalyst/g from example [m²/g] % % 11 15.24 1 66 1783 12 16.22 2 50 38 94 13 16.41 3 51 47 96 14 22.26 4 36 46 95 15 16.905 59 35 94 16 17.75 6 52 31 92 17 16.80 7 23 48 95

FIG. 1 shows activities and selectivities for the flame-synthesizedcatalysts (▴ example 13, ▪ example 17) and for the reference catalyst(−) in the autothermal dehydrogenation of propane to propene. In thecase of the catalyst (▪), only the support was produced by pyrolysis,and the support was subsequently subjected to wet-chemical impregnationas for the reference catalyst. The time in hours is plotted on theabscissa, and the conversions (40 to 50%) and selectivities (>80%) areplotted on the ordinate.

It can be seen that the three catalysts have comparable performance. Thereference catalyst has lower initial selectivities. However, over thetest cycles of a few weeks it equalizes to the catalysts according tothe invention. Thus, the flame-synthesized catalyst behaves like an agedcatalyst, which was produced by a conventional wet-chemical process.

1-17. (canceled)
 18. A catalyst particle, comprising platinum and tinand also at least one further element, selected from lanthanum andcesium, on a support comprising zirconium dioxide and optionally siliconoxide, wherein said catalyst particle is obtained by a method comprisingthe steps (i) preparing one or more solutions containing precursorcompounds of platinum, tin and the at least one further element,selected from lanthanum and cesium, and also of zirconium dioxide andoptionally silicon dioxide, (ii) converting the solution(s) to anaerosol, (iii) bringing the aerosol into a directly or indirectly heatedpyrolysis zone, (iv) carrying out pyrolysis with a gas, and (v)separating the catalyst particles formed from the pyrolysis gas.
 19. Thecatalyst particle of claim 18, wherein said catalyst particle contains0.05 to 1 wt. % Pt and 0.05 to 2 wt. % Sn.
 20. The catalyst particle ofclaim 18, wherein said catalyst particle has a specific surface of 36 to70 m2/g.
 21. The catalyst particle of claim 18, wherein said catalystparticles comprises 30 to 99.5 wt. % ZrO₂ and 0.5 to 25 wt. % SiO₂ assupport, and 0.1 to 1 wt. % Pt, 0.1 to 10 wt. % Sn, relative to the massof the support, La and/or Cs, wherein at least Sn and at least La or Csare contained.